US3508908A - Production of aluminum and aluminum alloys - Google Patents

Production of aluminum and aluminum alloys Download PDF

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Publication number
US3508908A
US3508908A US577473A US3508908DA US3508908A US 3508908 A US3508908 A US 3508908A US 577473 A US577473 A US 577473A US 3508908D A US3508908D A US 3508908DA US 3508908 A US3508908 A US 3508908A
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aluminum
alchlor
reductant
electrolyte
metal
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US577473A
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George Lang Herwig
Ernest Foley
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Commonwealth Scientific and Industrial Research Organization CSIRO
Conzinc Riotinto of Australia Ltd
Conzinc Riotinto Ltd
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Commonwealth Scientific and Industrial Research Organization CSIRO
Conzinc Riotinto Ltd
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/04—Dry methods smelting of sulfides or formation of mattes by aluminium, other metals or silicon
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C22B21/0038—Obtaining aluminium by other processes
    • C22B21/0046—Obtaining aluminium by other processes from aluminium halides
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium

Definitions

  • This invention relates to the production of aluminum and aluminum alloys from aluminum chloride (hereinafter referred to as alchlor) or from salts containing alchlor, and refers especially to a process of and apparatus for reducing a salt containing alchlor to aluminum by reaction with a metal reductant which may, for example, be magnesium.
  • the invention also includes a process and apparatus for the production of aluminum by fusion electrolysis using alchlor as the feed material.
  • the alchlor is preferably used in the form of a double salt, for example a low melting point double salt containing sodium chloride and alchlor.
  • double salt is used in the specification and claims hereof to include either (a) a double salt of alchlor and the halide of an alkali metal or (b) a solution of alchlor in a salt or salt phase.
  • the invention broadly resides in a process for the production of aluminum and aluminum alloys which comprises reacting a metallic reductant with a double salt of alchlor.
  • molten magnesum is reacted with a molten double salt of sodium chloride and aluminum chloride.
  • the reaction may be carried out in a reactor associated with an electrolytc cell in which case the magnesium chloride formed by the reaction may be treated electrolytically for recovery of magnesium and chlorine.
  • Electrolytic processes for the production of aluminum which are in present day use employ aluminum oxide as a solution in a double salt of sodium and aluminum 3,508,908 Patented Apr. 28, 1970 fiuorides.
  • Disadvantages of this system include 1) the Consumption of high purity carbon electrodes by the oxygen Component of the feed material at a rate which varies from 0.6 to 1.0 lb. of carbon per lb.
  • Alchlor is a volatile solid subliming at about 178 C. Although its vapour pressure may be lowered substantally in molten alkali metal chloride baths, alchlor is readily distilled from such baths when Operating at or about the melting point of aluminum (661 C.). As a consequence these processes are operated at low temperatures or under a positive pressure. Eutectic or low melting point fused salt mixtures containing alchlor have very poor electrical conductivity, especially below the melting point of aluminum.
  • Our invention in one of its aspects seeks to overcome the disadvantages of processes using electrolytes containing alchlor, while retaining the advantages of alchlor as a feed material, -by providing aprocess wherein little, if any, alchlor can ever be present in the electrolyte.
  • a process for the electrolytic production of aluminum and aluminum alloys comprises electrolysing a fused salt electrolyte containing at least one alkali metal halide using as cathode a molten metal or alloy, which molten metal or alloy contains in solution a metallic reductant deposted from the electrolyte, and Contacting the molten metal or alloy and the contained metallic reductant with a double salt of alchlor or 'with a solution of alchlor in a molten salt.
  • the electrolyte may contain one or more alkaline earth metal halides and/or rare earth metal halides.
  • the alchlor is contacted with the molten metal or alloy in such a manner that there is negligible alchlor entering the electrolysis compartment.
  • the invention includes a process for the electrolytic production of aluminum which comprises electrolysing in an electrolysis compartment or 'cell a fused salt electrolyte containing an alkali metal halide, the cathode being molten aluminum or aluminum alloy containing a metallic reductant deposited 'from the electrolyte by the electrolysis, transferring the molten aluminum or aluminum alloy and reductant to a reactor compartment or vessel, reacting alchlor with the metallic reductant in the reactor compartment or vessel, transferring the chloride product of the metallic reductant to the electrolysis compartment or cell, re-cycling molten aluminum containing a lower concentration of the metallic reductant back to the electrolysis compartment or cell, and discharging the molten metal product from the reactor compartment or vessel.
  • the electrolyte may contain one or more alkaline earth metal halides and/or rareearth metal halides in additio'to the alkali metal halide.
  • an impor'tant feature resides in effecti'ng the reacton between t'he'metallc reductant and the alchlor which latter is preferably in the vapour state, in a compartment or vessel which is distinct or separate from the electrolysis compartrnent, so that little or no alchlor is permitted to enter the electrolysis compartnent and consequently the possibility of "its loss with and contarnination of the chlorine produced in the electrolysis, and the attack by the alchlor on the anode material, are substantially prevented.
  • the reaction between the metallic reductant and the alchlor is effected in a two-stage reactor Compartment or vessel, wherein a salt phase capable of absorbing alchlor as a double salt simultaneously Contacts both the alchlor as vapour and the molten aluminum containing a metallic reductant.
  • a reaction occurs between the reductant and the alchlor double salt which results in a lowering of reductant concentration in the aluminum.
  • the alumnum from the first stage is re-cycled to the electrolysis compartrnent and the salt phase containing both the chloride product of the reductant and alchlor to saturation as a double salt or solution is contacted in a second stage to react to or approaching extinction with fresh molten aluminum and reductant from the electrolysis compartment.
  • the aluminum from the second stage passes back to the first stage 'while the salt phase containing the chloride product of the reductant but now denuded of alchlor is re-cycled to the electrolysis compartment.
  • a small portion of the electrolyte may be used as the alchlor-absor-bing salt phase, the portion of electrolyte being metered at such a rate to the first stage as to ensure that the salt phase leaving the second stage contains negligible amounts of alchlor.
  • two or more stages of contact may be used, in all cases alchlor being fed only to the first stage.
  • the two or more stage countercurrent reaction between the reductant electro deposited into the re-cycled aluminum and the alchlor double salt ensures that the salt phase leaving the reactor which is i re-cycled to the electrolysis compartment is essentially free of alchlor by last being in contact with an excess of reductant.
  • the aluminum working backto the first stage then still has a content of reductant suflicient for further reaction in this stage.
  • the salt phase In the first stage the salt phase is continuously in contact with the alchlor vapour and absorbs it as fast as the alchlor portion of the double salt reacts with the excess reductant.
  • the salt phase leaves the first stage for the later stages still with a content of alchlor to be removed by incoming reductant.
  • the quantity of alchlor reacted overall will be equivalent to the quantity, of reductant removed in the reactor, firstly, because there will be aflquantity of reductant in the first stage to react with 4 the alchlor Vapour being fed in, and secondly because the reductant present in the second stage will react with the alchlor (present as a double salt) to or approaching extinction.
  • alchlor cannot enter the electrolysis compartment in any appreciable quantity. Alchlor can only leave the first stage of the reactor as ⁇ a double salt and this can only be produced if reductant is reacted to the chloride in this stage. It follows that an excess of reductant must always exist in the later stages which will be capable of reacting essentially all of the alchlor out of the double salt. In the case of'an alkaline earth metal reductant electrolyte is metered into the first stage to form a double salt With the alchlor, the quantity metered being such as to achieve the above requirements.
  • the metallic cathode should comprise a metal or alloy which is molten within the required temperature range, which is a sufiiciently good solvent for the metallic'reductant used and which is substantially unreactive to alchlor.
  • Aluminum or an alloy of aluminum is preferably used.
  • a preferred feature of the invention is the employ- 'nent, as components of the fused salt electrolyte, of an alkali metal halide or mixture of alkali metal and alkaline earth metal halides.
  • composition of the fused electrolyte should desirably be such 'that the metal or metals deposited at the cathde during electrolysis (Le. the metallic reductant) have adequate 'solubility in the' molten metallic ca'thode (eg. in molten aluminum or aluminurn alloy),'low solubility in the saline phase, and, when dissolved "in the molten cathode metal, have suffic'ient reactivity to reduce alchlor vapour.
  • Magnesium chloride, or other alkali earth metals are used in admixture with the halides of sodum, potassium or other alkali metals.
  • alkali chlorides may be used alone or in admixture 'with each other.
  • alkali metal or alkaline earth metal halides specfically the chlorides and/or fluorides, may be added, within the limitations set out above; to modify and improve the properties of the electrolyte.
  • molten salt comprising either;
  • the aluminum plus reductant metal formed is transferred to a separate second compartment where it is reacted countercurrently with alchlor double salt under conditions of high, but not necessarily 100% efficiency.
  • Aluminum or aluminum alloy denuded in reductant is collected in suitable collection equipment from which it is either recycled to the electrolysis compartment to maintain the cathode metal at the desired level or tapped off, as required.
  • the temperature at which the electrolysis and reduction processes are carried out is desirably maintained at lO-100 C. above the melting point of the electrolyte, or the cathode metal or the salt phase -following the reducton process whichever is the highest.
  • a further feature of one form of the invention resides in enclosing the reactor compartment in such a manner that back pressure in the vapour or gas space is used to control the rate of alchlor addition; preferably the reactor compartment is totally enclosed to the gas phase, so that if an excess of alchlor is fed it accumulates as a gas and builds up pressure within the compartment. If the alchlor supply to this compartment is only at low pressure, then the accumulated pressure in the compartment retards or stops the flow of alchlor into the compartment and this state continues until suflicient of the excess alchlor vapour is consumed by fresh reductant contained in the liquid metal received from the electrolytic cell to reduce the back pressure and allow further flow. This is a very desirable feature as the alchlor feed rate is thereby automatically controlled according to demand.
  • the alloy may be produced by introducing the chloride of the element in addition to alchlor into the reactor compartment at the appropriate rate.
  • the process of this invention has a number of advantages over existing processes for the electrolytic produc tion of aluminum. It consumes virtually no carbon, continuously produces aluminum at high current efliciencies and enables operation at temperatures above the melting point of aluminum yet significantly below those used in current aluminum extractive technology. By the use of gaseous alchlor a high purity feed can be introduced and a closed cell Construction used with several attendant advantages.
  • EXAMPLE 1 A fused salt electrolyte comprising 20% w./w. magnesium chloride 40% w./w. lithium chloride and 40% w./w. sodum chloride was electrolysed at 670-700 C. in an alumina-lined cell fitted with a Vertical .carbon rod as anode and having a pool of commercial-grade aluminum as cathode.
  • the interpolar gap was 0.71 inch, the current density 1080 amps per square foot and the overall voltage 3.2 to 3.4 volts.
  • magnesium chloride content was replenished to 25% by adding additional molten magnesium chloride. Electrolyss was then continued for a further period of one hour after which the aluminum metal product was removed and on analysis was found to contain 397% w./w. metallic magnesium.
  • a reaction crucible was prepared by lining a mild steel crucible with high alumina refractory material.
  • the crucible was fitted with a vertical shaft carrying an impeller at its lower end.
  • the crucible and contents were placed in a steel retort, evacuated, filled with argon and then heated to 750 C. Pure gaseous aluminum chloride was then fed in at a controlled steady rate (1.5 litres per minute S.T.P.) to the atmosphere above the salt phase. At the same time the impeller was rotated to splash molten metal onto the wall of the crucible and thereby increase the contact between the molten metal and the salt at the interface.
  • the aluminum chloride was rapidly absorbed by the sodum chloride to form a double salt sodum aluminum chloride) and the contact between the double salt and the aluminum-magnesium alloy at the interface resulted in a reaction between the double salt and the magnesium to yield magnesium chloride and to return sodum chloride to the salt phase for absorption of further quantities of aluminum chlorde.
  • the metal reductant, magnesium is fed at a known rate into the upper section of a vertical reactor containing molten aluminum and fused sodium chloride.
  • Gaseous aluminum chloride is fed under pressure into the upper part of the reactor at a rate stoichiometrically equivalent to that of the magnesium.
  • Product metal is drawn off from the base of the reactor at a corresponding rate, whilst magnesum chloride overflows a weir at the top of the reactor and may be diverted to an electrolytic cell for regeneration of magnesium and chlorine.
  • the contents of the reactor are continuously agitated.
  • makeup magnesium may be added to the system as an alloy or pure metal may be blended into the recirculating stream.
  • EXAMPLE 3 85 gms. of magnesium ingot in a fused alumina crucible (8" X 3" diameter) were heated to 700 C. under an -argon atmosphere in a steel crucible. Lumps of a double salt of aluminum and sodium chlorides (74.8% aluminum chloride) were added as required to maintain the temperature in the range of 750 to 800 C. until a total of 592 gms. had been added, agitating continuously with a tantalum stirrer. After cooling, the solid saline and metallc phases were separated mechanically and analysed. The magnesium content of the metallc aluminum phase was less than 0.004%. The aluminum chloride content of the saline phase ranged from 16.6%
  • EXAMPLE 4 5275 gms. of an aluminum-magnesium alloy (90.4% magnesium) were heated to 700 C. as described in the Example 3; after which 289 gms. of a double salt of sodiurn and aluminum chlorides (73.7% aluminum chloride) were added progressively with st-irring. After cooling and separating the two phases, 517.5 gms. of aluminum Were obtained with a magnesium content of 0.004 to 0.04%; the 274 gms. of saline phase contained 3.1 to 37% aluminum chloride.
  • FIGURE 1 is a View in sectional elevation of apparatus for the electrolytic production of aluminum
  • FIGURE 2 is a sectional view taken on line 2-2 of FIGURE 1;
  • FIGURE 3 is a sectional plan view taken on line 3--3 of FIGURE 1.
  • the apparatus ind-icated generally at 1 is provided with an outer 'shell 2 which is thermally insulated by the lining 3.
  • An inner graphite and/or carbon lining 4 contains the contents of the apparatus and carries current from the connectors 6 to the cathodic liquid metal layer 7.
  • the sides of the electrolysis compartment or cell 11 are electrically insulated by a refractory lining 5.
  • the apparatus 1 is divided internally by graphite and/ or carbon wall '8 and by graphite carbon and/or refractory wall 9 into five compartments, narnely the electrolysis compartment 11, the pump compartment 12, the first stage reactor compartment or vessel 13, the second stage reactor compartment or vessel 14 and the product metal storage sump 15.
  • the electrolysis compartment 11 contains a molten salt electrolyte 16 which is of lower specific gravity than the cathodic metal layer 7 therebeneath.
  • Anodes 17, 18 preferably of graphite or carbon depend into the electrolyte 16 and are Secured to the cover 19, the anode connection being indicated at 20.
  • the undersurface of the cover 19 not protected by the anodes 17, 18 is line'd with refractory block 21.
  • a chlorine gas outlet 22 is fitted through the cover 19 and block 21 and communicates with the space above the electrolyte 16. Direct current is supplied to the connectors 6 and 20.
  • a cover 23 is fitted to the first and second stage reactor compartments, the pump Compartment and the product metal storage sump. Refractory block linings 24 are used to protect the undersurface of the cover 23. The covers 19 and 2.3 are sealed and gas tight. Refractory block lining 25 protects the walls of the reactor compartments 13, 14.
  • a similar passageway 30 for cathode metal and electrolyte extends between the electrolysis compartment 11 and the pump compartment 12.
  • a wall or bafie 31 is provided in the electrolysis compartment 11 and extends from the end of the said compart-ment which is nearest to pump compartment 12, to a point spaced a short distance from the opposite, end of the compartment 11.
  • the wall or baflle 31 forms 'a trough 32 between itself and the adjacent wall of the compartment 11.
  • the passageway 30 communicates with one end of the trough 32.
  • a wall or weir 33 between pump compartment 12 and product metal storage sump 15 controls the metal level throughout the system.
  • a downwardly slopng passageway 34 is provided in the bottom of sump 15 for periodic t-apping of product aluminum, the outlet from passageway 34 being normally closed by a removable plug 35.
  • a passageway 36 through which the cathode metal/ electrolyte interface passes, permits flow of electrolyte from the first stage reactor compartment 13 to the second stage reactor compartment 14 and permits flow of cathode metal in the opposite direction.
  • the flow of met-al is controlled by a lip 37 which is located inside the second stage reactor compar-tment 14 and rises above the cathode metal/electrolyte interface.
  • Metal is delivered from the second stage to the first stage by being splashed against the dividing wall by impeller 28 and then running down inside lip 37 and through assagew-ay 36.
  • a metal outlet passage 38 is provided to permit flow of -metal from the first stage reactor compartment 13 to the pump compartment 12, this pass-age being located below the surface of the met-al.
  • the pump compartment 12 is provided With -an electrolyte metering pump 39 of the gas displaeement type adapted to deliver electrolyte 16 entering pump compartment 12 through passage 30 at a controlled rate, when so required, through a passageway 40 to the first stage reactor compartment .13.
  • Alchlor vapour is supplied through the main supply pipe 41 ⁇ and reractory sparger pipes 42 which project downw ardly through the cover 23 into the first stage reactor compartment 13 terminating above the surface of the electrolyte.
  • the cell is filled with sufficient molten aluminum or aluminum 'alloy 7 to cover the bottom of the electrolysis compartment 11 and give good electrical contact with the lining 4.
  • a metallic reductant e.g. magnesium
  • sufficient molten electrolyte 16 is poured into the cell to cover the bottom of the anodes 17, 18.
  • the molten electrolyte comprises an alkali metal halide and may also include a selection of alkaline earth metal halides and rare earth metal halides. Preferably it contains sodium chloride.
  • the source of direct current is connected to the cell and electrolysis of the electrolyte 16 in the electrolysis compartment 11 takes place with deposition of metal reductant, e.g. magnesium, in the c-athodic layer 7, the metallic reducant entering into solution in the molten aluminum.
  • metal reductant e.g. magnesium
  • the electrolyte metering pump 39 and the impellers 28 are started to circulate electrolyte clockwise through the cell as seen in FIGURE 3 -and to circulate molten metal anti-clockwise as seen in the same figure.
  • alchlor vapour is fed from the main 41 through the pipe 42 into the atmosphere above the electrolyte in the first stage reactor compartment 13.
  • Pressure of alchlor in the main 41 is maintained at aconst-ant small positive value. This forces the vapour into the reactor chamber 13 until such time as the pressure built up in the gas space of the chamber is sufiicient to halt the vapour flow.
  • This pressure is relieved by further reaction of the alchlor vapour -in the gas space with the electrolyte more alchlor will feed from the main 41.
  • the alchlor forms -a double salt with the electrolyte, e.g. if the electrolyte is sodium chloride, sodium aluminum chloride is formed.
  • the electrolyte fiowing from the first stage reactor compartment 13 to the second stage reactor compartment 14 through passageway 36 consists of the double salt, e.g. sodium aluminum chloride, and a proportion of the chloride of the metallic reductant, e.g. magnesium chloride.
  • the double salt e.g. sodium aluminum chloride
  • the chloride of the metallic reductant e.g. magnesium chloride.
  • Molten metal comprising aluminum or aluminum .alloy and the metallic reductant, e.g. magnesium, enters the second stage reactor compartment 14 from the electrolysis compartment 11 through passageway 29.
  • the reductant concentration in the aluminum is lowered by a reaction between the reductant and the double salt.
  • sodium aluminum chloride reacts with magnesium to yield sodium chloride and magnesium chloride which are recycled through passageway 29 to the electrolysis compartment 11 where the magnesium chloride is electrolysed, the chlorine being discharged through outlet 22 and the magnesium going into solution in the aluminum in the cathode layer.
  • the sodium chloride is recycled to the first stage reactor compartment 13 by the metering pump 39 where it absorbs alchlor as described above to form the double salt sodium aluminum chloride.
  • the double salt reacts with the residual metallic reductant in the molten metal phase to yield the chloride of the metallic reductant described 'above as comprising -a proporton of the electrolyte circulated from the first stage reactor compartment 13 to the second stage reactor compartment 14.
  • a process for the production of aluminum and aluminum alloys which comprises electrolysing in an electrolysis zone a fused salt electrolyte containing at least one alkali metal halide, the cathode being molten aluminum or aluminum alloy containing a metal reductant deposited from the electrolyte by electrolysis, transferring the molten aluminum or aluminum alloy and reductant to a reactor zone, reacting a double salt of alchlor with the metallic reductant in the reactor zone, transfer'ing the chloride product of the metallic reductant to the electrolysis zone, re-cycling molten aluminum containing a lower concentration of the metallic reductant back to the electrolysis zone, and discharging the molten metal product from the reactor zone.
  • alchlor as vapour is contacted in the reactor zone with a salt phase capable of absorbing alchlor as a double salt.
  • a process for the production of aluminum and aluminum alloys which comprises electrolysing in an electrolysis zone a fused salt electrolyte containing at least one alkali metal halide and at least one halide selected from the group consisting of the akaline earth metal halides and the rare earth metal halides, the cathode being molten aluminum or aluminum alloy containing a metal reductant deposited from the electrolyte by electrolysis; transferring the molten aluminum or aluminum alloy and reductant and electrolyte as a molten salt phase to a reactor zone, reacting alchlor with the molten salt to yield a double salt and reacting the double salt with the metallic reductant in the reactor zone to yield the chloride product of the metallic reductant; transferring the chloride product of the metallic reductant to the electrolysis zone, re-cycling molten aluminum containing a lower concentration of the metallic reductant back to the electrolysis zone, and discharging the molten metal product from the reactor zone.
  • alchlor is fed to the first stage of a two-stage reactor zone, the aluminum or aluminum alloy from the first stage being re-cycled to the electrolysis zone and the salt phase containing both the chloride product of the reductant and the double salt being fed to the second stage of said reactor zone to react with fresh molten aluminum or aluminum alloy and reductant from the electrolysis zone.
  • a process for the production of aluminum and aluminum alloys which comprises electrolyzing a fused salt electrolyte containing at least one alkali metal halide, using as cathode a molten metal or alloy which contains in solution a metallic reductant deposited from the electrolyte, and Contacting the molten metal or alloy and the contained metallic reductant with a double salt of alchlor, the reaction between the metallic reductant and the double salt of alchlor being eifected in two stages, in which process the electrolyte and the molten metal are transferred from the electrolysis zone to the reactor zone in counter-current flow, the alchlor being fed to the first stage of the reactor zone, the electrolyte being'fed initially to the first stage of the reactor zone and thence to the second stage of the reactor zone and the molten metal being fed initially to the second stage of the reactor zone and thence to the first stage of the reactor zone.
  • a process for the production of aluminum and aluminum alloys wherein a fused salt electrolyte containing at least one alkali metal halide is electrolyzed using a cathode of a molten metal or alloy, in which the electrolyte comprises a halide of a metallc reductant for aluminum chloride which reductant is soluble in the cathode, the metailic reductant being deposited by electrolysis from the electrolyte and dissolved in the cathode, and the cathode metal or alloy and the contained reductant being brought into contact with a double salt of alchlor.
  • molten salt electrolyte is electrolyzed in an electrolysis cell and the cathode metal or alloy and the contained metallc reductant are transferred'to a reactor in which a double salt of alchlor is contacted with the metallc reductant to produce a chloride of the reductant, which chloride is transferred to the electrolysis ceil, the molten metal or alloy containing aluminum and a correspondingly lower concentration of metallic reductant, part of which is fed back to the electrolysis cell and part of which is discharged from the reactor as the molten metal product.
  • the electrolyte contains at least one halide of a metal selected from the group consisting of the alkaline earth metals and the rare earth metals.
  • reaction between the metailic reductant and double salt of alchlor is carried out in a reactor having two sections.

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US577473A 1965-09-08 1966-09-06 Production of aluminum and aluminum alloys Expired - Lifetime US3508908A (en)

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AU63759/65A AU412090B2 (en) 1965-09-08 1965-09-08 Production of aluminium and aluminium alloys
AU1029066 1966-08-29

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CH (1) CH493637A (xx)
ES (1) ES330982A1 (xx)
GB (1) GB1162153A (xx)
IS (1) IS704B6 (xx)
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3755099A (en) * 1971-09-08 1973-08-28 Aluminum Co Of America Light metal production
US5090998A (en) * 1989-12-20 1992-02-25 Alusuisse-Lonza Services Ltd. Purification of metal melts with halogen gas generated in an electrolysis cell
US11634829B2 (en) * 2016-11-24 2023-04-25 Obshchestvo S Ogranichennoy Otvetstvennost'Yu “Obedinennaya Kompaniya Rusal Inzhenerno-Tekhnologicheskiy Tsentr” Method for producing aluminum alloys

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010041084A1 (de) * 2010-09-20 2012-03-22 Sgl Carbon Se Elektrolysezelle zur Gewinnung von Aluminium
CN111118354A (zh) * 2020-03-13 2020-05-08 青海大学 金属镁还原法回收废铝屑的方法

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Publication number Priority date Publication date Assignee Title
US362441A (en) * 1887-05-03 X e eichaed geatzel
US387876A (en) * 1888-08-14 Aluminium bronze and other allots
US2742418A (en) * 1952-08-28 1956-04-17 Ethyl Corp Electrolytic cell for alkali-lead alloy manufacture
GB757908A (en) * 1952-06-24 1956-09-26 Reynolds Metals Co Process for producing aluminium electrolytically by amalgam metallurgy
US2919234A (en) * 1956-10-03 1959-12-29 Timax Associates Electrolytic production of aluminum

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US362441A (en) * 1887-05-03 X e eichaed geatzel
US387876A (en) * 1888-08-14 Aluminium bronze and other allots
GB757908A (en) * 1952-06-24 1956-09-26 Reynolds Metals Co Process for producing aluminium electrolytically by amalgam metallurgy
US2742418A (en) * 1952-08-28 1956-04-17 Ethyl Corp Electrolytic cell for alkali-lead alloy manufacture
US2919234A (en) * 1956-10-03 1959-12-29 Timax Associates Electrolytic production of aluminum

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3755099A (en) * 1971-09-08 1973-08-28 Aluminum Co Of America Light metal production
US5090998A (en) * 1989-12-20 1992-02-25 Alusuisse-Lonza Services Ltd. Purification of metal melts with halogen gas generated in an electrolysis cell
US11634829B2 (en) * 2016-11-24 2023-04-25 Obshchestvo S Ogranichennoy Otvetstvennost'Yu “Obedinennaya Kompaniya Rusal Inzhenerno-Tekhnologicheskiy Tsentr” Method for producing aluminum alloys

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LU51905A1 (xx) 1967-01-06
IS704B6 (is) 1970-03-20
GB1162153A (en) 1969-08-20
NL6612689A (xx) 1967-03-09
NO124841B (xx) 1972-06-12
BE686501A (xx) 1967-02-15
IS1602A7 (is) 1967-03-09
CH493637A (de) 1970-07-15
SE325714B (xx) 1970-07-06

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